EP0057575A2 - Methode zur Bildung stabilisierter Kohle-Öl-Gemische - Google Patents

Methode zur Bildung stabilisierter Kohle-Öl-Gemische Download PDF

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Publication number
EP0057575A2
EP0057575A2 EP82300447A EP82300447A EP0057575A2 EP 0057575 A2 EP0057575 A2 EP 0057575A2 EP 82300447 A EP82300447 A EP 82300447A EP 82300447 A EP82300447 A EP 82300447A EP 0057575 A2 EP0057575 A2 EP 0057575A2
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Prior art keywords
coal
oil
mixture
water
zone
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EP82300447A
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English (en)
French (fr)
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EP0057575A3 (en
EP0057575B1 (de
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Carl E. Eckman
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Standard Oil Co
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Gulf and Western Manufacturing Co
Standard Oil Co
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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L1/00—Liquid carbonaceous fuels
    • C10L1/32—Liquid carbonaceous fuels consisting of coal-oil suspensions or aqueous emulsions or oil emulsions
    • C10L1/322—Coal-oil suspensions

Definitions

  • the present invention relates to a method for forming stabilized coal-oil mixtures.
  • this invention relates to an improved method for forming coal-oil mixtures in stable form using selected conditions of elevated temperature and shear or high mixing.
  • this invention is directed to an improvement in a process for forming coal-oil mixtures wherein coal of significantly greater water content than heretofore thought acceptable is utilized to form coal-oil mixtures and wherein the amount of additives used to form the coal-oil mixture in the form of a gel is substantially reduced.
  • Coal is a most valuable form of energy. It is estimated that in the United States there is more energy available in coal than in petroleum, natural gas, oil shale, and tar sands combined. Recent energy shortages, together with the availability of abundant coal reserves and the continuing uncertainties in the availability of crude oil, have made it imperative that methods for converting coal into a more useful energy source be developed.
  • a number of methods are being explored for this purpose.
  • One such method employs gasification techniques, such as destructive distillation, to effect the conversion of coal to a low or medium Btu gas.
  • high pressure hydrogenation is utilized to liquefy the coal, making it more suitable for transport and burning.
  • the treated coal is then immediately separated from ash and sulfur and cleaned coal is recovered or, alternatively, formed into a liquid mixture, such as a coal-oil mixture.
  • the coal-oil mixture is thereafter treated with additional materials and a stabilizing agent to form a gel or thixotropic mixture, thereby providing a clean or relatively clean stable composition ready for transport, storage, burning or further processing.
  • the chemical surface treatment method achieves high separations of ash and sulfur using cleaning water, without significantly reducing the Btu value of the coal, a problem usually encountered when cleaning fine size coal with cleaning water, that is, the loss of coal in the cleaning water and the retention of water in the product coal.
  • the process is readily adapted for use at locations near or at the mine site, making it particularly suitable for reducing the transportation difficulties normally associated with coal.processing.
  • the chemical treatment of the coal is adapted to make the coal both hydrophobic and oleophilic. Coal particles so treated are readily separated from unwanted ash and sulfur using oil and water separation techniques.
  • the coal which is now substantially cleaned of ash and sulfur, is then dried to a water content level suitable for further processing or recovery.
  • the dried coal is thereafter formed into a coal-oil mixture, where it is again subjected to a chemical surface treatment using additional additives.
  • the coal-oil mixture is thereafter treated with a gelling agent to form the coal-oil mixture in the form a stable gel or thixotropic mixture.
  • the coal-oil mixture product thus produced is advantageously non-settling and enjoys a dispersion stability normally difficult to achieve and maintain without frequent stirring, the addition of further additives or an inordinate amountof fine grinding.
  • the mixture thus formed is thixotropic, allowing for ready pumpability on subjection to shearing or pumping forces.
  • the chemical surface treatment technique offers considerable advantages in providing coal as a useful energy source. Although the technique is attractive, however, it would be highly desirable that improvements be developed to make the process even more advantageous. For example, it would be highly desirable that the amount of drying which the cleaned coal is subjected to prior to forming the coal-oil mixture could be reduced, without adversely affecting the gel forming process. Such a decrease in drying would significantly improve the overall efficiency of the process, and advantageously would reduce or eliminate the need for burdensome and expensive drying equipment, such as large scale thermal dryers. Thermal drying equipment, e.g., is both unduly expensive and time consuming for large scale coal operations. The need for its use could seriously detract from the attractiveness of the process.
  • coal-oil mixtures can be formed from high water content coal using less reactant materials, by employing the chemical surface treatment technique and selected conditions of elevated temperature and shear.
  • coal is admixed with oil, monomeric compound, reaction initiator and reaction catalyst, at conditions of elevated temperature i.e., a temperature in excess of that heretofore considered desirable, and low shear.
  • elevated temperature i.e., a temperature in excess of that heretofore considered desirable, and low shear.
  • the mixture is thereafter immediately subjected to a condition of high shear at the same or nearly the same elevated temperature.
  • the coal-oil mixture is thereafter treated with a gelling agent to form a stable coal-oil mixture in the form of a gel or thixotropic mixture.
  • the condition of low shear is similar or nearly similar to conditions generally employed to slowly admix reactants under low speed stirring.
  • the shearing rate for such admixing is preferably less than about 1000 reciprocal seconds.
  • the condition of high shear requires the vigorous admixture or turbulence of materials such as in a high speed mixer or other device adapted to impart high shear mixing or agitation.
  • the condition of high shear exceeds about 1000 reciprocal seconds.
  • the elevated temperatures employed in the process range from about 145 to 195 °F. (63 - 91°C) and is most preferably from about 175 to 190°F.(79 - 88°C).
  • the time for mixing at the low shear conditions ranges from about 10 to 120, preferably about 30 to 60 seconds, and the time for mixing at the high shear condition ranges, from about 30 to 120, preferably about 60 to 90 seconds, although shorter times are contemplated for steady state operations.
  • the monomeric compounds employed in the process include unsaturated organic compounds such as ethylene, propylene, butylene, butadiene, styrene and the like as well as unsaturated carboxylic acids -and esters or salts thereof.
  • Reaction initiators that can be used include the free radical initiators such as water soluble salts, like copper nitrate or silver nitrate.
  • Suitable catalysts include the peroxides, such as hydrogen peroxide.
  • the liquid organic carriers that can be used in forming the coal-oil mixtures include commonly available organic fuel oils, such as number 2 or number 6 fuel oil. Gelling agents utilized to stabilize the coal-oil mixture are bases and include the hydroxides, such as sodium hydroxide, calcium hydroxide and the like.
  • the process of the invention is utilized to convert raw coal into coal-oil mixtures, using an initial pulverization step, a chemical surface treatment and separation step, and a drying step, to treat the raw coal prior to the formation of the coal-oil mixture.
  • the sequence of treatment steps for converting a coal product to a stabilized coal-oil mixture in accordance with the present invention, includes: an elevated temperature mixing and reaction zone 10; an elevated temperature high shearing zone 12, and a gelling zone 14. These zones can collectively be referred to as the coal-oil mixture forming section, represented by the numeral 16.
  • the sequence of treatment steps is shown with reference to an overall process for converting raw coal into a stabilized coal-oil mixture in accordance with the invention.
  • the process of the invention for converting raw coal into a stabilized coal-oil mixture includes: a pulverization zone 18, a chemical surface treatment and separation zone 20, a drying zone 24 and a coal-oil mixture forming section 16, comprised of, as mentioned previously, the elevated temperature mixing and reaction zone 10, the elevated temperature high shearing zone 12 and the gelling zore 14.
  • raw coal such as anthracite, bituminous coal, sub-bituminous coal, lignite and the like
  • pulverization zone 18 is introduced into pulverization zone 18 through line 26 wherein the raw coal is crushed and initially cleaned, usually in the presence of water, using conventional apparatus, such as ball mills, breakers and the like.
  • additives such as sodium pyrophosphate or sodium carbonate which assist in rendering the ash more hydrophilic to facilitate separation for reasons that will be immediately apparent.
  • additives are shown in Figure 2 to be introduced through line 29.
  • the water utilized during the pulverization operation is shown in the drawing to be introduced through line 28.
  • Rock and other unwanted products are removed from pulverization zone 18 through line 30.
  • the coal-water stream produced in pulverization zone 18 is typically in a coal to water ratio of about 1 to 19, preferably about 1:3, in the form of an aqueous slurry, the coal having a particle mesh size of approximately 48 to 300 mesh (0.295 to 0.05mm), preferably about 80% being of about 200 mesh Tyler Standard screen size (0.074mm).
  • unwanted ash and sulfur are still present in the coal, and it is desired to chemically treat the coal to facilitate the separation of coal from the ash and sulfur in a unitary or nearly unitary operation as will be discussed.
  • the coal-water slurry leaving pulverization zone 18 through line 32 is introduced into chemical surface treatment and separation zone 20 wherein the coal is chemically treated and separated from the ash and sulfur.
  • the coal is treated with monomeric compound in the presence of a liquid organic carrier, water and selected additives such as, reaction initiators and catalysts.
  • the coal thus treated is adapted to ready separation from ash and sulfur, preferably by oil and water separation techniques, because the additives employed make the treated coal hydrophobic and oleophilic, thus facilitating coal separation from ash and sulfur, which are generally hydrophilic.
  • the process of the invention utilizes two stages of "chemical surface treatment".
  • chemical surface treatment is undertaken in chemical surface treatment and separation zone 20, wherein raw coal is cleaned i.e., beneficiated.
  • the second chemical surface treatment occurs in elevated temperature mixing and reaction zone 10, which is employed in forming the coal-oil mixture.
  • the chemical surface treatment process used in the process herein is disclosed in great detail in heretofore-mentioned copending European application No.81300152.6. While it is not completely understood at this time and while not wishing to be bound by theory, it is believed that this surface treatment involves the formation of a polymeric organic coating on the surface of the coal of one or more monomeric units by molecular grafting or otherwise, of polymeric side chains on the coal molecules.
  • the chemical surface treatment materials include: "monomeric compound”; “reaction initiator”; “reaction catalyst” and “liquid organic carrier”, adapted for use in one or both of these two zones.
  • the particular compounds used in each zone can differ.
  • such monomers include ethylene, propylene, butylene, tetrapropylene, isoprene, butadiene, such as 1,4-butadiene, pentadiene, dicyclopentadiene, octadiene, olefinic petroleum fractions, styrene, vinyltoluene, vinylchloride, vinylbromide, acrylonitrile, methacrylonitrile, acrylamide, methacrylamide, N-methylolacrylamide, acrolein, maleic anhydride, maleic acid, fumaric acid, abietic acid, mixtures thereof and the like.
  • butadiene such as 1,4-butadiene, pentadiene, dicyclopentadiene, octadiene, olefinic petroleum fractions
  • styrene vinyltoluene
  • vinylchloride vinylbromide
  • acrylonitrile methacrylonitrile
  • acrylamide methacrylamide
  • a preferred class of monomers for the purposes of the present invention are unsaturated carboxylic acids, esters, or salts thereof, particularly, those included within the formula RCOOR' wherein R is an olefinically unsaturated organic radical, RCOOR' preferably containing from about 2 to about 30 carbon atoms, and R' is hydrogen, a salt-forming cation such as an alkali metal, alkaline earth metal or ammonium cation, or a saturated or ethylenically unsaturated hydrocarbyl radical, preferably containing from 1 to about 30 carbon atoms, either unsubstituted or substituted with one or more halogen atoms, carboxylic acid groups and/or hydroxyl groups in which the hydroxyl hydrogens may be replaced with saturated and/or unsaturated acyl groups, the latter preferably containing from about 8 to about 30 carbon atoms.
  • RCOOR' wherein R is an olefinically unsaturated organic radical, RCOOR' preferably containing from about
  • Specific monomers conforming to the foregoing structural formula include unsaturated fatty acids such as oleic acid, linoleic acid, linolenic, ricinoleic, mono-, di- and tri-glycerides of one or more unsaturated fatty acids and other esters of unsaturated fatty acids, acrylic acid, methacrylic acid, methyl acrylate, ethylacrylate, y ethylhexylacrylate, tertiar/butyl acrylate, oleylacrylate, methylmethacrylate, oleylmethacrylate, stearylacrylate, stearylmethacrylate, laurylmethacrylate, vinylstearate, vinylmyristate, vinyllaurate, soybean oil, dehydrated castor oil, tall oil, corn oil and the like.
  • unsaturated fatty acids such as oleic acid, linoleic acid, linolenic, ricinoleic, mono-
  • tall oil and corn oil have been found to provide particularly advantageous results. Corn oil is especially preferred.
  • compositions containing compounds within the foregoing formula and in addition containing, for example, saturated fatty acids such as palmitic, stearic, etc. are also contemplated herein.
  • chemical surface treatment agent connotes a wide range of compounds and entities adapted for use in the invention.
  • chemical surface treatment agent includes reaction initiators, reaction catalysts, combinations of reaction initiators and reaction catalysts and combinations of reaction initiators and combinations of reaction catalysts.
  • Reaction initiator connotes a wide range of compounds known to initiate free radical reactions.
  • any of those disclosed in the prior art may be used.
  • some of these initiators include, for example, sodium perchlorate and perborate, sodium persulfate, potassium persulfate, ammonium persulfate, silver nitrate, water soluble salts of noble metals such as platinum and gold, and water soluble salts of iron, zinc, arsenic, antimony, tin and cadmium and combinations of these materials.
  • Particularly preferred initiators herein are the water soluble copper salts, i.e. cuprous and cupric salts, such as copper acetate, copper sulfate and copper nitrate.
  • cupric nitrate cupric nitrate,.Cu(N0 3 ) 2 .
  • Further initiators contemplated herein are metal salts of naphthenates, tallates, octanoates, etc. said metals including copper, cobalt, chromium, mercury, manganese, nickel, tin, lead, zinc, iron, rare earth metals and mixed rare earths.
  • reaction catalyst employed in the coal surface treating reaction are any such materials commonly used in polymerization reactions.
  • any ctalytic amount of those catalysts which are commonly referred to as free radical catalysts or catalyst system (which can also be referred to as addition polymerization catalysts, vinyl polymerization catalysts or polymerization initiators) are preferred.
  • catalysts contemplated herein include benzoyl peroxide, methylethyl ketone peroxide, tertbutylhydroperoxide, hydrogen peroxide, ammonium persulfate, di-tert-butylperoxide, tert-butylperbenzoate, peracetic acid and, including such non-peroxy free radical initiators as the diazo compounds, such as 1-1-bis-azo-isobutyro nitrile and the like.
  • the surface treating reaction mixture of the present invention also includes a liquid organic carrier.
  • This liquid organic carrier is utilized to facilitate contact of the surface of the coal particles with the reactants.
  • liquid organic carriers included within the scope of this invention are, for example, fuel oil, such as No. 2 or No.
  • fuel oils other hydrocarbons including benzene, toluene, xylene, hydrocarbons fractions such as naphtha and medium boiling petroleum fractions (boiling point 100°-180°C), dimethylformamide, tetrahydrofurane, tetrahydrofurfuryl alcohol, dimethylsulfoxide, methanol, ethanol, isopropyl alcohol, acetone, methylethyl ketone, ethyl acetate and the like and mixtures thereof.
  • fuel oil is a preferred carrier.
  • Treatment in chemical surface treatment and separation zone 20 utilizes vigorous admixing of the coal slurry and reactants such as by mixing, injection, spraying or pumping action, to cause agitation, aeration and froth in the mixture.
  • the sequence for admixing the coal slurry, oil, water, monomeric compound, reaction initiator and reaction catalyst can be varied. However, it is generally desirable to introduce the coal-water slurry into a mixture of liquid organic carrier, monomeric compound and cleaning water, followed by the introduction of reaction catalyst and then reaction initiator.
  • the pulverized coal-water slurry is introduced into chemical surface treatment and separation zone 20 through line 32 where it is contacted with the monomeric compound introduced through line 34; reaction catalyst introduced through line 36; reaction initiator introduced through line 38; organic liquid carrier introduced through line 40 and cleaning water introduced through line 48.
  • the first chemical surface treatment reaction occurs in this zone during the admixing of the materials and the coal particles are made hydrophobic and oleophilic.
  • the hydrophobic and oleophilic characteristics of the treated coal are utilized to separate the coal from the unwanted ash and sulfur, which are both normally hydrophilic. This is readily effected utilizing the tendency of the ash and sulfur to enter the water phase. In this manner, the coal can be separated from the ash and sulfur by conventional operations adapted to separate oil from water.
  • a particularly effective technique for separating the treated coal particles from the unwanted ash and sulfur in the water phase is an aeration spray method wherein a coal froth phase is formed by spraying or injecting the treated or untreated coal-water slurry into the surface of cleaning water through spray nozzles at a spaced- apart distance from the water surface so as to form a turbulent. region producing aeration and a frothing or foaming of the coal particles.
  • the reactants are introduced into one or more froth flotation units.
  • the reactants can be separately introduced into the froth flotation units or they can be admixed beforehand in lines leading to the units.
  • the coal-water slurry is introduced into the vessel through pressure nozzles which facilitate the separation of ash from the coal by assisting in breaking up flocs of coal which are formed during chemical treatment..
  • a froth phase ensues, which rises to the surface of the water in the froth flotation unit carrying the cleaned coal with it.
  • the coal froth can then be skimmed from the water surface to effect the separation of the coal from ash and sulfur, which remain in the cleaning water.
  • the "chemical surface treatment” method offers considerable advantage in that the chemical reaction is made to occur simultaneously with the separation of the ash and sulfur. As a further advantage, a greater amount of ash and sulfur separation is achieved because the coal is treated in a fine size. Generally, admixing such fine size coal in the presence of water would seriously devalue the Btu content of the coal. The chemical surface treatment method, however, provides a ready separation from water and therefore maintains the high Btu value of the coal.
  • FIG. 3 illustrates one unit 44 suitable for use in chemical surface treatment and separation zone 20.
  • the coal slurry enters the unit 44 through lines 32, through nozzles 43.
  • Cleaning water enters through line 48 and reaction initiator, reaction catalyst, monomeric compound and liquid organic carrier enter through lines 38, 36, 34 and 40, respectively.
  • Frothing takes place, thus providing a coal froth'phase and a water phase.
  • the coal froth phase is skimmed from the water surface and removed through line 46.
  • the procedure in froth flotation unit 44 can be repeated (preferably about two further times) until a cleaned coal stream is formed. It may not be necessary to repeat the chemical surface treatment in any repeated froth flotation steps.
  • reaction conditions utilized in vessel 44 will vary depending on the materials employed. Generally the unit is operated at temperatures of from 20 to 90 °F. (-7 to 32°C) and at atmospheric or nearly atmospheric pressure.
  • the coal, cleaned in chemical surface treatment and separation zone 20 be dried or substantially dried. It has been generally considered that coal having too high a water content would be unsuited to the formation of stable coal-oil mixtures. Excess water has been considered to seriously impare the gelling operation needed to form the stable coal-oil mixture.
  • the amount of drying required for the water ladened coal is significantly reduced by virtue of a unique coal-oil mixture forming technique. In this way, less energy is needed to dry the coal and the need for burdensome and expensive drying units is substantially reduced.
  • the treated coal is now hydrophobic and oleophilic making drying even less burdensome. Drying can therefore be readily effected using conventional mechanical dryers, and not expensive and time consuming thermal dryers. All of these features making the process of the invention even more attractive.
  • the cleaned coal is removed from chemical surface treatment and separation zone 22 through line 46 and is introduced into drying zone 24 to remove
  • the apparatus utilized in drying zone 24 are readily available and can include conventional centrifugal driers, vacuum driers and the like.
  • the treated coal leaving drying zone 24 and having a water content of approximately 15%, based on the weight of dry coal, is then introduced into the coal-oil mixture forming section 16.
  • the first step it is desired to admix the coal with oil to form the coal-oil mixture, and preferably to again chemically surface treat the coal. This is effected under conditions of elevated temperature and low shear or mixing.
  • the coal-oil mixture is immediately subjected to a condition of high shear or mixing at the maintained elevated temperature.
  • the dry coal leaving drying zone 24, which as a result of treatment is in powder form, is introduced into elevated temperature and reaction zone 10, through line 52, where it is admixed in a suitable mixing vessel (not shown) with oil introduced through line 54.
  • the amount of coal in the admixture can vary from 5% by weight coal to 70% by weight.
  • the coal is admixed in an amount of about 50% by weight.
  • Monomeric compound introduced through line 56, reaction initiator introduced through line 58 and reaction catalyst introduced through line 60 are added to the coal-oil mixture at this point.
  • the reactants, including the monomeric compound, reaction initiator, and reaction catalyst, utilized in elevated temperature and reaction zone 10 are the same type as those utilized in chemical surface treatment and separation zone 20, and have been described previously.
  • the preferred reactants for use in elevated temperature and reaction zone 10 include tall oil as the monomeric compound; a solution of benzoyl peroxide in toluene as the reaction catalyst; a solution of cupric nitrate in water as the reaction initiator; and No. 2 fuel oil as the oil used in major amounts to form the coal-oil mixture.
  • the proportions of each of these materials can vary.
  • the amounts of materials used are approximately, by weight,about 5 to 1000 parts per million (ppm) preferably 5-10 ppm of reaction initiator; and about 2.5 to 500 parts per million (ppm), preferably 2.5-5 ppm of reaction catalyst.
  • the monomeric compound is utilized in zone 10, according to the invention, in very low amounts of from about .2% to about 5%, preferably about 1.0 to about 3%, based on the total weight of the coal-oil mixture.
  • the procedure for admixture of the reactants can vary. In one technique the monomeric compound is first admixed with the oil. Reaction initiator is then introduced, followed by the addition of reaction catalyst. Alternatively, all of the reactants can be admixed in one step.
  • Admixture of the reactants in elevated temperature and reaction zone 10 is conducted at elevated temperatures and under conditions of low shear.
  • low shear connotes a general admixture of components under conditions suitable for thorough contacting of the constituents.
  • the condition of low shear utilized in this zone is generally less than 1000 reciprocal seconds.
  • high shear connotes the vigorous admixture, turbulent mixing, mixing or high agitation of coal-oil mixtures. Generally, the condition of high shear is greater than 1000 reciprocal seconds and preferably greater than 4500 reciprocal seconds.
  • elevated temperature refers to temperatures from about 145 to 195°F, (63 to 91°C) and more preferably from 175 to 190°F (79 to 88°C).
  • the time period for mixing in elevated temperature mixing and reaction zone can vary. Generally, admixing is done in a period of from about 10 seconds to about 30 minutes and preferably from about 30 to 60 seconds, although the invention is adapted to both steady state and batch operations so that the residence time can vary widely.
  • a wide variety of apparatus can be used in elevated temperature and reaction zone 10.
  • One suitable apparatus is a stainless steel vessel having associated stirring means and a steam heated jacket.
  • the coal-oil mixture leaves elevated temperature mixing and reaction zone 10 through line 62 and is introduced into elevated temperature high shearing zone 12.
  • a high shearing apparatus is employed to admix the coal-oil mixture at the desired (63 to 91°C) elevated temperatures of from about 145 to- 195°F/, preferably (79 to 88°C) 175-190°F/, and at high shearing.
  • One high shearing apparatus suitable for use in zone 12 is the "Dicon" mixer available from the W. H. Potter Co., Model No. 3MS5.0004.
  • the high shear mixing in zone 12 immediately follow the low shear mixing in zone 10 so little time, if any, is provided for the coal to settle in the coal-oil mixture.
  • the period for high shear mixing in zone 12 will vary. But generally, high shear mixing is done in periods of from about 10 seconds to about 30 minutes and preferably about 60 to 90 seconds, although the invention is adapted to both steady state or batch. operations so that the residence times can vary widely.
  • a gelling agent can be employed for this purpose.
  • the gelling agent uniquely combine with the dispersed coal, making the mixture even more stable and the possibility of coal settling even less likely.
  • the highly sheared coal-oil mixture leaves elevated temperature high shearing zone 12 through line 64 and is introduced into gelling zone 14 where selected gelling agents are added to form the stable coal-oil mixture in the form of a gel or thixotropic mixture.
  • gelling agents can be used in gelling zone 14 and include: organic and inorganic bases, such as sodium hydroxide, calcium hydroxide, potassium hydroxide, ammonium hydroxide and the like.
  • organic and inorganic bases such as sodium hydroxide, calcium hydroxide, potassium hydroxide, ammonium hydroxide and the like.
  • the preferred gelling agent for use in gelling zone 14 is sodium hydroxide, preferably diluted in water to a 33% concentration. These materials can be added as such, or in the form of aqueous solution.
  • the gelling agent is gradually added to the mixture.
  • the gelled coal-oil mixture is withdrawn as a product from gelling zone 14 through line 68 as a highly stable coal-oil mixture, having excellent non-settling properties and a high Btu burning capacity.
  • the mixture is useable in this form or it can be subjected to further treatment such as shearing to maintain a uniform coal distribution in the mixture.
  • the resulting mixture is stable, thixotropic and gel like, yet it is readily flowing upon subjection to shearing or pumping forces.
  • Examples 1-3 generally show the process steps for producing particular types of treated coal product suitable for forming the coal-oil mixtures according to the invention although other treated or untreated coals can be used.
  • the procedures of Examples 1-3 follow the process steps in Figure 2, beginning with the pulverization treatment and up to the elevated temperature mixing and reaction zone 10.
  • the cleaning procedure is repeated two further times using cleaning water and skimming the frothed- coal from the water surface.
  • the coal is then dried to a water content of 15.4%, based on the weight of dry coal, using a Buchner filter.
  • Example 1 The procedure of Example 1 is repeated using equivalent amounts of (a) styrene monomer; (b) oleic acid; and (c) dicyclopentadiene; substituted for corn oil.
  • a cleaned coal product is produced having a moisture concentration of 15% based on the weight of dry coal.
  • Example 1 The procedure of Example 1 is repeated using (a) Poco- hontas coal; (b) Taggart coal and (c) Lower Freeport coal substituted for Pittsburgh Seam coal. A cleaned coal product is produced having a moisture concentration of 20% based on the weight of dry coal.
  • the mixture is stirred at the "low" speed range for 30 seconds. During the 30 second period two cubic centimeters of a 0.1% solution of a cupric nitrate in water solution and one cubic centimeter of a benzoyl peroxide (0.1%) in toluene solution are added to the mixture. After the 30 second period, the solution is mixed in the waring blender at the "high" speed rate for a period of 60 seconds.
  • the mixture is then transferred to a stainless steel vessel fitted with a mixer and a heating element.
  • the mixture is slowly stirred and maintained at a temperature of l90°F. While stirring, to the mixture is added 3.8 cubic centimeters of a 33% sodium hydroxide solution in water over a 15 second period using a laboratory buret. Stirring of the mixture is continued for a 1.5 minute period.
  • Example 4 The procedure of Example 4 is repeated utilizing corn oil and styrene in equivalent amounts in substitution for tall oil.
  • a stable coal-oil mixture is produced each time.
  • Example 4 The procedure of Example 4 is repeated except that an equivalent amount of hydrogen peroxide is utilized in substitution for benzoyl peroxide as the reaction catalyst.
  • a stable coal-oil mixture is produced each time.
  • the technique of the present invention provides stable coal-oil mixtures using coals having a water content 15% or higher.
  • coals unbeneficiated or treated by the variety of conventional cleaning techniques can be introduced directly into the elevated temperature mixing and reaction zone 10 for the formation of the stable coal-oil mixture.

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  • Oil, Petroleum & Natural Gas (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
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EP82300447A 1981-01-29 1982-01-28 Methode zur Bildung stabilisierter Kohle-Öl-Gemische Expired EP0057575B1 (de)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
US06/230,064 US4306883A (en) 1981-01-29 1981-01-29 Process for forming coal-oil mixtures under selected conditions of temperature and shear
US230064 1981-01-29

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EP0057575A2 true EP0057575A2 (de) 1982-08-11
EP0057575A3 EP0057575A3 (en) 1983-08-10
EP0057575B1 EP0057575B1 (de) 1986-04-09

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US (1) US4306883A (de)
EP (1) EP0057575B1 (de)
JP (1) JPS57145182A (de)
AU (1) AU546229B2 (de)
CA (1) CA1184762A (de)
ZA (1) ZA82216B (de)

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP3678215A1 (de) 2019-01-07 2020-07-08 Andreas Stihl AG & Co. KG Zellverbinderaufbau, akkupack und garten- und/oder forstbearbeitungssystem
EP3678214A1 (de) 2019-01-07 2020-07-08 Andreas Stihl AG & Co. KG Aufbau, akkupack und garten- und/oder forstbearbeitungssystem

Families Citing this family (19)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4406664A (en) * 1980-01-22 1983-09-27 Gulf & Western Industries, Inc. Process for the enhanced separation of impurities from coal and coal products produced therefrom
US4304573A (en) * 1980-01-22 1981-12-08 Gulf & Western Industries, Inc. Process of beneficiating coal and product
US4583990A (en) * 1981-01-29 1986-04-22 The Standard Oil Company Method for the beneficiation of low rank coal
US4306883A (en) * 1981-01-29 1981-12-22 Gulf & Western Manufacturing Company Process for forming coal-oil mixtures under selected conditions of temperature and shear
AU551441B2 (en) * 1981-01-29 1986-05-01 Standard Oil Company, The Coal-aqueous (oil) mixtures
CA1194304A (en) * 1981-05-28 1985-10-01 Lester E. Burgess Beneficiated coal, coal mixtures and processes for the production thereof
US4526585A (en) * 1981-05-28 1985-07-02 The Standard Oil Company Beneficiated coal, coal mixtures and processes for the production thereof
CA1214039A (en) * 1982-09-30 1986-11-18 George E. Snow Process for the beneficiation of carbonaceous matter employing high shear conditioning
US4622046A (en) * 1982-09-30 1986-11-11 The Standard Oil Company Stabilized high solids, coal-oil mixtures and methods for the production thereof
US5096461A (en) * 1989-03-31 1992-03-17 Union Oil Company Of California Separable coal-oil slurries having controlled sedimentation properties suitable for transport by pipeline
US7279017B2 (en) 2001-04-27 2007-10-09 Colt Engineering Corporation Method for converting heavy oil residuum to a useful fuel
US7341102B2 (en) 2005-04-28 2008-03-11 Diamond Qc Technologies Inc. Flue gas injection for heavy oil recovery
US20070128251A1 (en) * 2005-12-07 2007-06-07 Piedmont Pharmaceuticals, Inc. Process for manufacturing chewable dosage forms for drug delivery and products thereof
US7955632B2 (en) 2005-12-07 2011-06-07 Bayer B.V. Process for manufacturing chewable dosage forms for drug delivery and products thereof
ATE491861T1 (de) 2006-02-07 2011-01-15 Diamond Qc Technologies Inc Mit kohlendioxid angereicherte rauchgaseinspritzung zur kohlenwasserstoffgewinnung
DE112007002839A5 (de) * 2006-09-22 2009-09-10 Herbert Georg Nopper Verpresster Brennstoff aus nachwachsenden organischen Rest- und/oder Rohstoffen und Verfahren zu dessen Herstellung
AU2012258681A1 (en) * 2011-05-24 2013-12-19 Soane Mining, Llc Recovering valuable mined materials from aqueous wastes
CA3209907C (en) 2016-04-04 2024-04-09 Arq Ip Limited Solid-liquid crude oil compositions and processes
US9777235B2 (en) 2016-04-04 2017-10-03 Allard Services Limited Fuel oil compositions and processes

Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB155212A (en) * 1914-02-16 1922-03-09 John James Victor Armstrong Process of making a liquid fuel
FR745506A (de) * 1933-05-12
US4101293A (en) * 1977-03-30 1978-07-18 Reichhold Chemicals, Inc. Stabilizing emulsifiers
GB2009783A (en) * 1977-12-05 1979-06-20 Energy & Minerals Res Co Thixotropic Gel Fuels Containing Ash Modifiers
US4165969A (en) * 1973-02-23 1979-08-28 Ashland Oil, Inc. High carbon content liquid fuels
EP0032811A2 (de) * 1980-01-22 1981-07-29 The Standard Oil Company Verfahren zur Aufbereitung von Kohle und aufbereitetes Kohleprodukt
US4306883A (en) * 1981-01-29 1981-12-22 Gulf & Western Manufacturing Company Process for forming coal-oil mixtures under selected conditions of temperature and shear

Family Cites Families (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3401049A (en) * 1964-05-25 1968-09-10 Polymer Res Corp Of America Method of grafting polymerizable monomer onto substrates and resultant article
US3698931A (en) * 1969-06-18 1972-10-17 Polymer Research Corp Of Ameri Method of grafting polymerizable monomers onto substrates
US4252639A (en) * 1979-11-05 1981-02-24 Otisca Industries, Ltd. Coal beneficiation processes
US4033852A (en) * 1975-06-26 1977-07-05 Polygulf Associates Process for treating coal and products produced thereby

Patent Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR745506A (de) * 1933-05-12
GB155212A (en) * 1914-02-16 1922-03-09 John James Victor Armstrong Process of making a liquid fuel
US4165969A (en) * 1973-02-23 1979-08-28 Ashland Oil, Inc. High carbon content liquid fuels
US4101293A (en) * 1977-03-30 1978-07-18 Reichhold Chemicals, Inc. Stabilizing emulsifiers
GB2009783A (en) * 1977-12-05 1979-06-20 Energy & Minerals Res Co Thixotropic Gel Fuels Containing Ash Modifiers
EP0032811A2 (de) * 1980-01-22 1981-07-29 The Standard Oil Company Verfahren zur Aufbereitung von Kohle und aufbereitetes Kohleprodukt
US4306883A (en) * 1981-01-29 1981-12-22 Gulf & Western Manufacturing Company Process for forming coal-oil mixtures under selected conditions of temperature and shear

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP3678215A1 (de) 2019-01-07 2020-07-08 Andreas Stihl AG & Co. KG Zellverbinderaufbau, akkupack und garten- und/oder forstbearbeitungssystem
EP3678214A1 (de) 2019-01-07 2020-07-08 Andreas Stihl AG & Co. KG Aufbau, akkupack und garten- und/oder forstbearbeitungssystem

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CA1184762A (en) 1985-04-02
US4306883A (en) 1981-12-22
EP0057575A3 (en) 1983-08-10
EP0057575B1 (de) 1986-04-09
ZA82216B (en) 1982-12-29
JPS57145182A (en) 1982-09-08
AU7947482A (en) 1982-08-05
AU546229B2 (en) 1985-08-22

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